PROCESS AND APPARATUS FOR ENHANCING DISTRIBUTION OF NOX-REDUCING CHEMICALS IN A HIGH-SOLIDS ENVIRONMENT

Abstract: Reduction of nitrogen oxides emissions from large scale combustors, such as coal-fired boilers and incinerators which produce effluents with high solids concentrations, is improved. High solids loading and other operational factors can cause such large temperature gradients transverse to the direction of effluent flow the SNCR cannot be practiced in conventional fashion. The process entails defining a near-wall zone having a temperature effective for SNCR and a central zone where the temperature is too high. NOx-reducing composition is introduced into the effluent within the near-wall zone in fine droplets (30 and 130) and can be introduced into the central zone after the gas has cooled or as large droplets effective to survive the high temperature.

Description: PROCESS AND APPARATUS FOR ENHANCING DISTRIBUTION OF NO z -REDUCING CHEMICALS IN A HIGH-SOLIDS ENVIRONMENT DESCRIPTION Technical Field The invention relates to reducing the environmental damage caused by large-scale combustion, and provides im¬ proved processes and apparatus for achieving this, especial¬ ly in the field of NO x reduction by selective noncatalytic reduction (SNCR) in effluents where influences such as high solids contents create large temperature gradients trans¬ verse to the direction of flow. The oxides of nitrogen (N0 X ) contribute to smog, ground level ozone formation, and acid rain. The major sources of anthropogenic N0 X emissions are stationary and mobile com¬ bustion of carbonaceous materials, such as coal, oil and gas, as well as refuse and organic industrial chemicals. These materials are burned at such high temperatures (e.g., 1000° to 1700 β C) in large scale combustors, that the conditions favor formation of free radicals of oxygen and nitrogen and their chemical combination as nitrogen oxides. Titles 1, 3, and 4 of the Clean Air Act Amendments of 1990 address the control of N0 X emissions from stationary sources to limit ground level ozone and acid rain. To reduce the emission of NO x/ both primary and sec¬ ondary measures have been employed. Primary measures are those which modify combustion itself and may involve using an excess of air or fuel or a combination of both in staged combustion. However, such measures are typically expensive and present only partial remedies. A number of economically-attractive secondary measures have been developed which enable combustion under efficient conditions, with resultant NO x generation, but then reduce the NO x by converting it to other compounds which can either be emitted or eliminated from the flue gas. Of these, selective gas phase reactions — both catalytic (SCR) and non-catalytic (SNCR) — are advantageous because they permi NO x reduction while using relatively low levels of chemical reducing agents. The SNCR procedures are especially effec¬ tive and economical for many applications, especially those where particulates could cause fouling of catalysts. However, the attainment of consistent, high reductions in NO x with SNCR procedures is a matter of considerable engineering and chemistry, especially where large tempera¬ ture gradients occur across a plane where chemical injectio is desired, such as in effluents containing high levels of entrained solids. These SNCR reactions occur in the gas phase and typically involve NO x levels of 20 to 1500 parts per million by volume (pp and either urea or ammonia at from one to three times the amount stoichiometrically re¬ quired. The reactions require mating of the reactive mate- rials in high dilution in the gas phase at the correct temperature. Typically, the NO x -reducing agents are introduced in aqueous droplets. For best results, the water must be evaporated from the droplets and the active agent converte to the gas phase to achieve contact with the NO x molecules the temperature range effective for reaction, e. g. , from 850" to 1150 β C. In the cases of coal-fired furnaces and those which require the injection of solid adsorbents to control the emission of sulfur oxides (SO , it has now be determined that the high levels of solids that become en¬ trained in the effluent gases can create such extreme cros sectional temperature gradients that SNCR procedures which attempt chemical injection across the entire cross section of an effluent passage, are rendered inefficient and produ tive of secondary pollutants. Unfortunately, space limita tions and combustor geometry often greatly limit injector location to just such circumstances. High levels of entrained solids affect the dynamics o evaporation of the water from treatment droplets and relea of the active chemicals. Results have often been inconsis tent when conventional means have been used in high solids environments, even where the desired temperature conditio were apparently being met. Temperature gradients of from 100* to 350*C, and greater, can be created by the tendenc of the solids to attenuate or refract the transmission of radiation from the gas to the heat absorbing surfaces. T can make some areas of a cross section too cold and other too hot. If too cold, the droplets can impact the equipm surfaces and/or form undesirable by-products such as ammo nia, and, if too hot, the active chemical can be oxidized form further N0 X . There is a need for improved distribution of active SNCR chemicals in combustion effluents which exhibit large cross-sectional temperature gradients, such as those heavi loaded with entrained particulates. Background Art Prominent among the SNCR processes are those disclose by Lyon in U.S. Patent 3,900,554 and by Arand et al in U.S. Patents 4,208,386 and 4,325,924. Briefly, these patents disclose that ammonia (Lyon) and urea (Arand et al ) can be injected into hot combustion gases to selectively react wi NO x and reduce it to diatomic nitrogen and water. The SNCR process described by Lyon reduces the concen tration of nitrogen monoxide (NO) . Lyon discloses injecti ammonia or certain ammonia precursors, or aqueous solution of either, into an oxygen-rich waste gas for selective reaction with the nitrogen monoxide at a temperature in th range of from 870" to 1100 β C. While the lower temperature limit can be reduced by the addition of certain substances it is important that the temperature of the combustion effluent lie within a narrow "temperature window" during t contact with the gaseous ammonia to achieve maximum utiliz tion of the ammonia for reduction of NO. Inefficient util zation increases costs and causes other problems associate with ammonia discharge, such as reaction with the sulfur t form solid ammonium sulfate and/or bisulfite which deposit on heat exchange surfaces and can quickly reduce heat tran fer efficiency. Arand et al disclose in U.S. Patent 4,208,386 that ur can be added alone or in solution to oxygen-rich effluents in a temperature range from 700" to 1100'C. Similarly, in U.S. Patent 4,325,924, Arand et al describe an SNCR proces utilizing urea in fuel-rich combustion effluents. Any ure which fails to react with NO x within the defined temperature windows is, nonetheless chemically transformed by heat arid some, during cooling, results in ammonia formation. A number of other patents define methods for operating at temperatures outside of the narrow ranges defined above for SNCR. For example, in U.S. Patent 4,992,249, Bowers discloses that if droplet size is increased and urea concen¬ tration is decreased, good results can be achieved in oxy¬ gen-rich effluents at higher temperatures than disclosed by Arand et al . And, in U.S. Patent 4,719,092, Bowers disclos¬ es that an additional material, an oxygen-containing hydro¬ carbon, can be introduced with the urea solution to reduce residual ammonia concentration in the effluent. Despite the ability of these processes to move the temperature window either higher or lower, the opening in the window remains fairly constant and distribution of the active chemicals at the operative temperature remains important. These patents do not recognize the difficulties in achieving suitable dis¬ tribution where the temperature gradients across the plane of intended chemical introduction are too great. Various nozzles and injectors have been designed to provide better distribution of chemicals into injection passages; however, without an understanding of the present invention, the achievement of satisfactory chemical distri¬ bution will remain an extremely difficult task. The recog¬ nition that operational factors such as entrained solids cause a predictable departure from conventionally understood temperature distributions, is essential to effective control of SNCR processes. Disclosure of Invention It is an object of the invention to improve the intro¬ duction and utilization of pollutant-reducing chemicals in effluents which are characterized by large temperature gradients in the direction transverse to flow, such as particulate-laden combustion effluents. It is another object of the invention to improve the reliability of SNCR NO x -reducing installations which depend on the introduction of aqueous solutions of NO x -reducing agents into combustion effluents which contain large amounts of entrained solids. It is another object to mitigate utilization and dis¬ tribution problems associated with SNCR processes in coal- fired installations. A yet further, but related, object is to mitigate utilization and distribution problems associated with SNCR processes in installations employing sorbent injection for S0 X reduction. These and other objects are achieved by the present invention which provides an improved process for reducing the concentration of nitrogen oxides in a flowing stream of combustion effluent, comprising: determining the tempera¬ ture at a plurality of points on a plane transverse to the flow of combustion effluent; based on the determined temper¬ atures, defining a near-wall zone which has an average temperature effective for N0 X reduction by selective noncat¬ alytic reduction utilizing a suitable NO x -reducing composi¬ tion, and a central zone having an average temperature above the effective NO x -reducing temperature with that composition and introducing NO x -reducing composition into the effluent for reaction within the near-wall zone. The process has particular application in the treatment of effluents laden with entrained particulate solids, such as those from coal- and other solid fuel-fired combustors and those which have been contacted with solid sorbents for S0 X reduction. It is important to employ the process of the invention where the difference between the average temperatures of the two zones is greater than about 100"C, and especially where the temperature difference is 200 β C or higher. At least a portion of the NO x -reducing composition is introduced into the near-wall zone as fine droplets of an aqueous solution, preferably the droplets being of a size effective to assure evaporation of substantially all of the aqueous carrier within the near-wall zone. In one preferred embodiment, NO x -reducing composition i also introduced as medium-to-large diameter aqueous droplets with a size, momentum and concentration to pass into and through the central zone without significantly reacting until the temperature of the effluent in that zone is re¬ duced to a level effective for NO x reduction. The concen¬ tration of the water and active NO x -reduction composition in the droplets which enter the central zone at high temper¬ ature, are selected for the droplet size range and injection velocity so that the water protects the active composition during high-temperature residence. The water should be sufficiently evaporated upon entering the lower temperatures downstream to quickly release the active NO x -reducing compo¬ sition within the effective temperature range. Introductio of small as well as large droplets can be achieved with a single or a multiplicity of injectors, as desired. It is also preferred that the above process be employe as the first stage of a multi-stage process. Desirably, a second stage injection of the same or a different composi¬ tion can be utilized to further reduce NO x or other pollut- ant. Third and subsequent stages can be employed as de¬ sired. In another embodiment, an excess of NO x -reducing compo sition can be effectively employed in the near-wall zone to maximize NO x -reduction and produce ammonia slip. This is effective where ammonia by-product is mixed by convective currents with at least a portion of the central zone efflu¬ ent after it has been cooled to an effective temperature fo reaction. Brief Description of the Drawings The invention will be better understood and its advan¬ tages will become more apparent when the following detaile description is read in conjunction with the accompanying drawings, in which: Figure 1 is a vertical cross section of a large scale combustor showing isotherms at a representative load condi tion and one arrangement of injectors for introducing acti chemicals for reducing N0 X in accordance with the invention and Figure 2 is a three-dimensional view showing isotherm in a large scale combustor as surfaces and showing multipl level injection, with injectors at each level positioned a several locations around the combustor perimeter as would necessary to provide good coverage of active chemical. Best Mode for Carrying out the Invention Effluents in need of treatment are produced by a vari ety of sources including large industrial and utility boil ers, incinerators, circulating fluidized bed boilers, and the like. Some of these, like coal- and wood-fired boiler will naturally produce effluents with high solids loadings. Others, such as those burning oil with significant sulfur content, produce effluents with high S0 X contents which are treated by dry or wet injection of sorbents such as calciu carbonate, calcium bicarbonate, lime, or the like. It wil be understood, however, that the invention is applicable .i any high temperature environment where high temperature gradients, such as caused by the presence of entrained solids, interfere with the reduction of nitrogen oxides by selective gas-phase reaction. Figure 1 depicts a vertical cross-section of a large- scale combustor 10 and shows isotherms determined within t effluent at a representative load condition. Burner 20 is shown to create a combustion flame 22 by burning a fuel su as coal with combustion air near the bottom of the combus¬ tion chamber 12. Hot combustion gases form an effluent which moves upwardly from the flame. For the purpose of definition, the term "effluent passage" is meant to includ the entire structure through which the hot combustion gase flow, including the combustion chamber 12, vertical passag 14, horizontal passage 16, and subsequent structure (not shown) . As the effluent rises, zones of differential tempera¬ ture develop due to a number of influences — significant among which are the effect of heat exchange through efflue passage walls and particulate solids entrained within the hot gases. The entrained solids near the heat absorbing walls tend to radiate heat efficiently over short path lengths. Thermal radiation from the central portions of t gas is refracted or otherwise attenuated by the entrained solids. Figure 1 shows representative isotherms, e. g. at 1300'C, 1200°C, 1050 β C and 950 β C, illustrating temperature gradients greater than 200" to 350"C and more at some hori¬ zontal cross sections where the measurable temperatures""nea the walls would be apparently ideal for SNCR, typically fro 950° to 1050"C. Temperature gradients of these magnitudes make ineffective those SNCR procedures which attempt injec¬ tion of uniformly-sized droplets to achieve uniform coverag across a plane transverse to the direction of flow. It is typical in the case of effluents with high solid loadings (e.g., greater than 5 grams/normal cubic meter) that the difference between the average flue gas tempera¬ tures near the wall and near the center of the unit is at least about 100"C, typically at least 200"C, and can be 350"C or more higher. At least a portion of the NO x -reduci composition is preferably introduced into the near-wall zon at this location as fine droplets of an aqueous solution, t assure evaporation of substantially all of the aqueous carrier from these droplets within the near-wall zone. In most cases, a least some of the droplets should be larger and be injected at sufficient velocity to enter the central zone and survive until they pass through it. The present invention calls for determining the tem¬ perature of the effluent at a sufficient number of location that a temperature profile can be determined to define a near-wall zone where the temperature conditions favor SNCR reactions, and a central zone where the temperature is too high. This can be accomplished by means of a suction pyrom eter employing a k-type thermocouple. It is also desired t determine effluent velocities at a sufficient number of locations to permit the use of a suitable computational fluid dynamics (CFD) modeling technique to establish a three-dimensional temperature profile, such as illustrated in Figure 2, to determine the best location within the near wall zone for introducing the NO x -reducing composition. Fo applications with construction in the future or where direc measurements are impractical, CFD modeling alone can suffi¬ ciently predict furnace conditions. The injection locations into the near-wall zone, and the droplet velocity, size and concentration, are facilitat¬ ed by computational fluid dynamics and chemical kinetic modeling (CKM) techniques. In reference to the CFD and CKM techniques, see the following publication and the references cited therein: Sun, Michels, Stamatakis, Comparato, and Hofmann, "Selective Non-Catalytic N0 X Control with Urea: Theory and Practice, Progress Update", American Flame Re¬ search Committee, 1992 Fall International Symposium, Octobe 19-21, 1992, Cambridge, MA. Figure 1 shows one arrangement of injectors for intro¬ ducing active chemicals for reducing N0 X in accordance with the invention. Two levels of injection are shown, but the invention can be carried out with a single zone where condi tions permit. Typically, however, it is preferred to emplo multiple stages. This permits both the injection of differ ent compositions simultaneously or the introduction of compositions at different locations or with different injec tors to follow the temperature variations which follow changes in load. See in this regard, U.S. Patent 4,777,024 to Epperly et al . The location of injection and chemical formulation can be varied to meet the temperature and com¬ positional variations in the gas stream being treated as described in U.S. Patent 4,780,289 to Epperly et al . Desir ably, a second stage injection of the same or a different composition is employed to further reduce NO x or other pol¬ lutant. Third and subsequent stages can be employed as desired. In Figure 1, a first level of introduction 30 is illus trated as providing sprays having a droplet size distribu¬ tion which includes smaller droplets for shallow penetratio into the near-wall zone and larger droplets with deeper penetration into the central zone. For practical purposes with urea solutions, the near-wall zone is preferably from about 950" to 1050" C, and the central zone will include the higher temperatures, at this level. The other level of introduction illustrated as 130, is farther downstream and is shown as providing a spray which again penetrates only the near-wall zone at that location. The exact location of the sprays and their spray patterns can be determined for optimum results by computational fluid dynamics tech¬ niques — given an appreciation of the distinct temperature zones which occur, such as in high solids environments and an understanding that the different horizontal cross- sectional temperature zones must be treated separately. In most SNCR processes, the treatment composition is introduced into the effluent by an injector which generally comprises a conduit, sometimes fitted at the tip with a nozzle, extending into an effluent gas stream. In some cases a portion of effluent or other gas is employed to help atomize and disperse the treatment composition. The spray or injection pattern is defined with precision, often mea¬ sured with the aid of computerized data acquisition to assure good distribution and reaction. Apparatus of varying degrees of sophistication are known. Some comprise coaxial, multi-tubular structures, such as those disclosed by Burton in U.S. Patent 4,842,834, by DeVita in U.S. Patent 4,985,218, and by Chawla et al in WO 91/17814, the disclo¬ sures of each of which are incorporated herein by reference. Injectors of these and other designs can be used to achieve the desired injection pattern, droplet sizes, droplet con¬ centrations and droplet velocities to achieve the objective of the invention. Typically, in SNCR processes an attempt is made to penetrate the effluent stream with complete coverage in a plane transverse to the direction of effluent flow. The present invention helps improve operation by defining a ' near-wall zone having suitable temperatures for SNCR and introducing active chemicals into that zone, despite the fact that hotter than desired temperatures exist on that same plane. The improvement is facilitated by introducing fine droplets to be utilized in the near-wall zone and la∑rg droplets which enter the central zone but survive until the reach a lower temperature zone downstream. Referring again to Figure 2, a plurality of injectors 230 will typically be employed around the perimeter of the combustor. The injectors are.preferably spaced one from th other as uniformly as is consistent with effectiveness whic will vary with velocity and temperature profiles within the effluent passage. Typically, to achieve uniform coverage with fine droplets in the near-wall zone, nozzles will be spaced from about 1 to about 3 meters apart. While not shown, for clarity, it is also desired to inject larger droplets at at least the first stage. Introduction of smal as well as large droplets can be achieved with a single or multiplicity of injectors, as desired. The coverage of the central zone, which is hotter than the near-wall zone, is accomplished by injecting the NO x - reducing composition farther downstream (where the effluent has cooled) or by injecting larger droplets at relatively low concentration and high velocity so that they survive th higher temperatures and release the active agent farther downstream where the temperature is more suitable for SNCR. When operated optimally, chemical utilization is increased, undesired by-products are decreased, and the chances for impingement with and damaging of heat exchange and other equipment surfaces is greatly reduced. Droplet sizes indicated below are determined with a Malvern 2600 instrument, utilizing a Fraunhofer diffraction laser-based system. And, unless otherwise indicated, all parts and percentages are based on the weight of the compo¬ sition at the particular point of reference. It is preferred that at least a portion (e. g. , at leas 10%) of the NO x -reducing composition be introduced into the near-wall zone in a form to have its intended effect there¬ in. Preferably, it is dispersed from a nozzle to provide uniformly fine droplets, e. g. having an average droplet siz within the range of from about 5 to about 100 microns Saut mean diameter. The concentration of the active chemical a water in the fine droplets should permit complete release within this zone. Thus, relatively high concentrations of NO x -reducing chemical, e. g. 20 to 50%, are preferred for th purpose. Droplet injection velocities are not particularl important if sizes are small enough, but can reasonably be in the range of from 5 to 60 m/sec. It is also preferred that a portion of the NO x -reducin composition which is introduced into the near-wall zone of suitable reaction temperature, be injected so as to pass through the near-wall zone and into the central zone. Because the central zone is too hot for good SNCR reaction the droplets should be of a size, concentration and veloci effective to pass through the portion of the zone which is too hot, survive until lower temperatures prevail downstre and there release the active chemical. The concentration the water and active NO x -reducing composition in the dropl which enter the central zone at high temperature are selec ed so that the water protects the active composition durin high-temperature residence. The water should be sufficien ly evaporated upon entering the lower temperatures down¬ stream to quickly release the active NO x -reducing composit within the effective temperature range. For these purpose the droplets will preferably be of a size of from 100 to 1000, e. g. from 100 to 500 microns Sauter mean diameter, a concentration of from 2 to 35% active NO x -reducing agent, ideally of low volatility such as urea, and a velocity of from about 10 to 60 m/sec. It is an advantage of the present invention that liquid droplets comprising NO x -reducing agents can be injected at well-controlled particle size distributions and velocities to make at least a portion of the active agent available near the point of injection in the near-wall zone while yet providing, as desired, droplets which will enter the central zone and survive desired temperature window for NO x reduc¬ tion. This distribution of droplets can be accomplished using one or more injectors. Well-controlled polydispersity of droplet sizes will provide optimum results following the teachings of the invention. The NO x -reducing agent is most desirably introduced as an aqueous treatment solution, such as urea or other NH-con- taining compositions, and can include one or more enhancers. The various treatment solutions are premixed to include the NO x -reducing composition and enhancer most appropriate for the range of temperatures expected to be encountered. The total amount of the reducing agent injected into the effluent from all points should be sufficient to obtain a reduction of the nitrogen oxide concentration. In partic¬ ular, the reducing agents are employed in total amounts sufficient to provide a molar ratio of reducing agent to baseline nitrogen oxide content (i.e., prior to treatment at that stage) of about 1:4 to about 5:1. The ratio is prefer¬ ably within the range from 1:2 to 3:1, even more narrowly 2:3 to 2:1. In most situations this amount will be distrib¬ uted jointly by a number of nozzles from a number of points as illustrated in Figure 1. In one embodiment, an excess of NO x -reducing compositio can be effectively employed in the near-wall zone to maxi¬ mize N0 X reduction and produce ammonia slip. This is effec¬ tive where ammonia by-product is mixed by convective cur¬ rents with at least a portion of the central zone effluent after it has been cooled to an effective temperature for reaction. Various NH-containing compositions, in their pure and typical commercial forms, will generate effective gas- phase agents (e. g. , the amidogen radical) for SNCR when introduced in aqueous solution and subjected to elevated temperatures. Among the prominent NH-containing composi¬ tions are those selected from the group consisting of ammo¬ nia, urea, urea precursors, urea hydrolysis products, prod¬ ucts of reaction of urea with itself or other compositions, related compositions, and mixtures of these. Among these compounds are ammonium carbonate, ammonium formate, ammoniu citrate, ammonium acetate, ammonium oxalate, other ammonium salts (inorganic and organic) particularly of organic acids, ammonium hydroxide, various stable amines, guanidine, guani dine carbonate, biguanide, guanylurea sulfate, melamine, dicyanimide, calcium cyanamide, biuret, 1,1-azobisformamide, methylol urea, methylol urea-urea, dimethyl urea, hexamethy lenetetramine (HMTA) , and mixtures of these. Among the hydrolysis products are ammonia, carbamates such as ammonium carbamate, ammonium carbonate, ammonium bicarbonate and other ammonia salts, various urea complexes and half ammonia salts. The exact form of some of these compounds is not known because the techniques employed to analyze them can affect their makeup. U.S. Patent 4,997,63 to Hofmann et al and PCT application WO 92/02291 to von Harpe et al , are incorporated herein by reference. Enhancers are additive materials which modify the effectiveness of a pollutant-reducing agent in terms of its effective temperature window, its utilization efficiency, o the like. Among the enhancers are the above materials when used in suitable combination, oxygenated hydrocarbons, and mixtures of these. Exemplary of the oxygenated hydrocarbons are ketones, aldehydes, alcohols including polyols, carbox¬ ylic acids, sugars, starch hydrolysates, hydrogenated starch hydrolysates, sugar-containing residues such as molasses, and mixtures of any of these. The entire disclosures of U.S. Patents 4,719,092, 4,844,878 and 4,877,591 are incorpo¬ rated herein by reference. It is an option to incorporate in the solutions of the invention, a hardness-suppressing composition comprising at least one member selected from the group consisting of polymers, phosphonates, chelants, phosphates and mixtures of any two or more of these, in an amount effective to suppress hardness. Thus, single members of this group can be em¬ ployed where effective, or two or more members of a single group can be employed, as well as mixtures of members from different groups. Surfactants and stabilizers are also employed. The disclosure of Dubin et al U.S. Patent Appli¬ cation No. 07/770,857, filed October 3, 1991, is incorporat¬ ed herein by reference. Control of liquid droplet sizes can be facilitated by chemical as well as mechanical means. For example, the addition of surfactants can help provide smaller average droplet sizes as disclosed in U.S. Patent Application Serial No. 07/959,706 filed October 13, 1992 by D. Diep and L. Lin. Also, the addition of certain polymers can help provide larger droplet sizes as disclosed in U.S. patent Application Serial No. 07/959,705 filed October 13, 1992 by D. Diep, L. Lin and P. Christiansen. The various injectors and nozzles can be tested at various flow rates and pressures to deter¬ mine their effect on droplet sizes. The NO x -reducing compositions will typically be prepare and shipped as a concentrate which is diluted for use. Typically, these concentrates will contain 25 to 65% urea, and 0.05 to 1.0 % of an effective hardness-suppressing composition. The urea and a separate additive package can be preblended to form this concentrate. This concentrate is typically diluted prior to injection as required to achieve a urea concentration effective under the injection condi¬ tions. Typically, dilution to concentrations of from 1 to 35% urea are effective. Typically, the pH of the aqueous solution is above 5, and generally is within the range of from 7 to 11, e. g. , 8 to 10. The above description is for the purpose of teaching the person of ordinary skill in the art how to practice the invention. It is not intended to detail all of those obvi¬ ous modifications and variations which will become apparen to the skilled worker upon reading the description. It is intended, however, that all such obvious modifications and variations be included within the scope of the invention which is defined by the following claims. The claims are meant to cover the claimed components and steps in any se¬ quence which is effective to meet the objectives there intended, unless the context specifically indicates the contrary.

Claims: CLAIMS 1. A process for reducing the concentration of nitrogen oxides in a flowing stream of combustion effluent, compris¬ ing: determining the temperature at a plurality of points o a plane transverse to the flow of combustion effluent; based on the determined temperatures, defining a near- wall zone which has an average temperature effective for N0 X reduction by selective noncatalytic reduction utilizing a suitable NO x -reducing composition, and a central zone which has an average temperature higher than suitable for N0 X reduction with that composition; and introducing NO x -reducing composition into the effluent within the near-wall zone. 2. A process according to claim 1 wherein the average temperature in the near-wall zone is at least 200"C lower than the average temperature in the central zone. 3. A process according to claim 1 wherein the average temperature in the near-wall zone is at least 350"C lower than the average temperature in the central zone. 4. A process according to claim 1 wherein the effluent is laden with entrained particulate solids. 5. A process according to claim 4 wherein the effluent is from a coal-fired or other solid fuel-fired combustor. 6. A process according to claim 4 wherein the effluent includes entrained solid sorbents introduced for S0 X reduc¬ tion. 7. A process according to claim 1 wherein at least a por¬ tion of the N0 x -reducing composition is introduced into the near-wall zone as fine droplets of an aqueous solution, the droplets being of a size effective and concentration to assure evaporation of substantially all of the water within the near-wall zone. 8. A process according to claim 7 wherein at least a por¬ tion of the NO x -reducing composition is introduced as medium to large diameter aqueous droplets with a size, momentum and concentration effective to cause the droplets to pass into and through the central zone without significantly reacting until the temperature of the effluent in that zone is re¬ duced to a range effective for N0 X reduction. 9. A process according to claim 8 wherein the introduction of fine and large droplets is accomplished by the same injector. 10. A process according to claim 8 wherein a multiplicity of injectors is employed to introduce large and fine drop¬ lets. 11. A process according to claim 1 wherein NO x -reducing composition comprises an NH-containing composition. 12. A process according to claim 11 wherein the NO x -reducin composition comprises an aqueous solution of a member se¬ lected from the group consisting of ammonia, urea, urea precursors, urea hydrolysis products, carbamates, ammonium carbonate, ammonium bicarbonate, cyanurates, ammonium salts of organic acids, other amidozine-generating compositions and mixtures of these. 13. A process according to claim 12 wherein the NO x -reducin agent comprises urea or at least one of its hydrolysis products or a salt thereof. 14. A process for reducing the concentration of nitrogen oxides in a flowing stream of combustion effluent laden with entrained particulates at a level of at least 5 g/Nm 3 , com¬ prising: determining the temperature at a plurality of points on a plane transverse to the flow of combustion effluent; based on the determined temperatures, defining a near wall zone which has an average temperature effective for N0 X reduction by selective noncatalytic reduction utilizing a suitable NO x -reducing composition, and a central zone which has an average temperature at least 300"C higher than that of the near-wall zone; and introducing NO x -reducing composition into the effluent, at least a portion being injected into the near-wall zone as fine droplets, wherein said NO x -reducing composition comprises an aqueous solution of a member selected from the group con¬ sisting of ammonia, urea, urea precursors, urea hydrolysis products, carbamates, ammonium carbonate, ammonium bicarbon¬ ate, cyanurates, ammonium salts of organic acids, other amidozine-generating compositions and mixtures of these, and said fine droplets being of from 5 to 100 microns Sauter mean diameter. 15. A process according to claim 14 wherein at least a portion of the NO x -reducing composition is introduced as medium to large diameter aqueous droplets with a size, momentum and concentration effective to cause the droplets to pass into and through the central zone without signifi¬ cantly reacting until the temperature of the effluent in that zone is reduced to a range effective for N0 X reduction. 16. A process according to claim 14 wherein the effluent is from a coal-fired or other solid fuel-fired combustor. 17. A process according to claim 14 wherein the effluent includes entrained solid sorbents introduced for S0 X reduc¬ tion. 18. A process for reducing the concentration of nitrogen oxides in a flowing stream of combustion effluent laden with entrained particulates at a level of at least 5 g/m 3 , com¬ prising: determining the temperature at a plurality of points on a plane transverse to the flow of combustion effluent; based on the determined temperatures, defining a near- wall zone which has an average temperature effective for N0 X reduction by selective noncatalytic reduction utilizing a suitable NO x -reducing composition, and a central zone which has an average temperature at least 300"C higher than that of the near-wall zone; and introducing NO x -reducing composition comprising an aqueous solution of an active component which is a member selected from the group consisting of ammonia, urea, urea precursors, urea hydrolysis products, carbamates, ammonium salts of organic acids, other amidozine-generating composi¬ tions and mixtures of these; at least a portion of said composition being introduced into said near-wall zone in droplets of a size of from 5 to 100 microns Sauter mean diameter and at a concentration of from 50 to 98% water, and at least a portion of the N0 X - reducing composition is introduced as medium to large diame¬ ter aqueous droplets with a size of from 100 to 1000 mi¬ crons, and momentum and concentration effective to cause th droplets to pass into and trough the central zone without significantly reacting until the temperature of the effluen in that zone is reduced to a range effective for NO x reduc¬ tion, said concentration of the active NO x -reduction compo¬ sition in the droplets enter and which pass through the central zone at high temperature is selected so that the water in the droplets protects the active component during high-temperature residence in the central zone and is suffi¬ ciently evaporated upon entering the lower temperatures down stream to quickly release the active NO x -reducing compositio within the effective temperature range. 19. A process according to claim 17 wherein the average temperature in the near-wall zone is at least 350"C lower than the average temperature in the central zone. 20. A process according to claim 17 wherein the effluent is from a coal-fired or other solid fuel-fired combustor.

Inventors: COMPARATO JOSEPH R, MICHELS WILLIAM F, SUN WILLIAM H, COMPARATO, JOSEPH, R., MICHELS, WILLIAM, F., SUN, WILLIAM, H.
Applicants: NALCO FUEL TECH
Application year: 1994
Main classification: C01B21
IPC codes: B01D53